Method and apparatus for drying wet bio-solids using excess heat from a cement clinker cooler

ABSTRACT

Method and apparatus for drying wet bio-solids by utilizing waste heat from a clinker cooler in a cement making process.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a Continuation-in-Part of U.S. patent applicationSer. No. 10/866,999 filed Jun. 14, 2004.

BACKGROUND OF THE INVENTION

The present invention pertains to use of bio-solid materials as a fuelor fuel additive in a cement making process. In particular, the presentinvention pertains to incorporating drying of the wet bio-solidmaterials in a conventional cement making process and cement makingapparatus.

Bio-solids are defined as residual by-products from biological activityor the residual by-products from processing of biological materials.Materials that are of interest for use in the method and apparatus ofthe present invention include sewage sludge, paper pulp residue,industrial sludges, food processing sludges and agricultural wastesludges.

Conventional cement making processes e.g. the manufacturing processesand apparatus for the manufacture of Portland Cement, are based upon theprocessing of limestone (CaCO₂) by heating to achieve a cement clinkerwhich is basically calcium oxide (CaO) chemically bound with othermaterials such as alumina, silica and iron.

In a conventional Portland Cement manufacturing process the main rawingredient limestone is prepared with or without smaller amounts ofmaterials containing alumina, silica and iron and are ground to producewhat is called a raw meal. The meal is then conducted to apyro-processing area, which may include preheaters and calciners tocondition the raw meal for introduction into a rotary kiln where theintermediate product clinker is produced. The main kiln and thepreheaters and calciners are conventionally heated with a burner usingcoal, oil or gas as the fuel component. The coal, oil or gas isgenerally mixed with preheated combustion air and ignited to provide theheat necessary to decarbonate and melt the raw meal to produce clinker.At the discharge end of the conventional rotary kiln, the hot clinker isintroduced into a clinker cooler wherein large amounts of air are blownthrough the hot clinker to cool it to a temperature of about 200° F.After sufficient cooling the clinker can be ground into a final product.In the grinding operation of the cooled clinker a small amount of gypsummay be added to produce the finished Portland Cement.

One of the largest cost items in the manufacture of cement is the costof fuel. With ever increasing prices for coal, oil and gas alternatefuel sources are constantly be sought for use in the process.

Among the materials which have been considered for use as alternatefuels are bio-solid materials, which have been processed prior todelivery to the cement manufacturing plant to remove moisture so thatthe dried bio-solid materials are of a moisture content and size to beintroduced into the combustion processes for the cement manufacturingprocess.

U.S. Pat. No. 4,627,877 discloses a method and apparatus forcontinuously producing cement clinker. Patentees disclose use of wastematerial as fuel in a cement manufacturing process. The method andapparatus of the '877 patent provide for a cooling of cement clinker andthe use of recovered energy to promote heat decomposition of combustiblematerial.

U.S. Pat. No. 6,436,157 discloses a method for gasification ofbio-sludge. The intracellular water of the bio-sludge material isreduced by heating the bio-sludge material at a temperature sufficientto weaken the bacterial cell walls. The water-reduced concentratedbio-sludge may then serve as a fuel source. Heating is accomplished byusing a heat exchanger with details of the heat exchange process setforth at column 4, lines 47-67 of the '157 patent. The heating processis by a direct heat exchange, however, there is no disclosure of usingindirect heat exchange with heat taken from a clinker cooler in a cementmanufacturing process.

U.S. Pat. Nos. 5,895,213; 5,201,652; and 3,836,321 all describe variousclinker cooling devices used to recover heat energy from the cementclinker being cooled. The heat recovered from the clinker cooler can beused in other parts of the process such as preheating.

U.S. Pat. No. 5,862,612 discloses a method and system for dewateringcarboniferous materials using a vaportight pressure chamber. Water boundby capillary forces in fiber cells is reduced by a thermal mechanicaldewatering process. Patentees describe a dewatering process involvingthree steps, the first of which is heating of the high porous organicmaterial at an elevated temperature and at a high pressure thus reducingthe moisture of the solid material. Patentees rely on high temperatureand high pressure to effect dewatering of the material which may be usedas a fuel. However, there is no disclosure of coupling this process witha cement manufacturing process.

U.S. Pat. No. 4,702,745 is directed to a process for dewatering highmoisture content porous organic solids. Patentees process involves threesteps, the first of which is heating the high moisture content porousorganic solid at elevated temperature and high pressure to reduce themoisture content of the solid. Here again, there is no relationship ofthis process to a cement manufacturing process.

U.S. Pat. Nos. 1,965,513; 2,879,983; 4,285,140; 5,890,888; and 6,083,404disclose methods for upgrading a material by drying using varioustechniques.

SUMMARY OF THE INVENTION

The present invention pertains to a method and apparatus forincorporating wet bio-solids into a conventional cement making processso that the wet bio-solids can be brought to the cement manufacturingfacility where they are dried and conditioned for use as a fuel or fueladditive in the cement making process.

The wet bio-solids are dried using heat derived from the cement clinkercooler. Heat from the cooler is extracted by a heat exchange fluid whichis introduced into a contact dryer used to dry the wet bio-solids.

In an alternate embodiment heat from the cement clinker cooler isintroduced into the inlet of a rotary dryer with wet bio-solid sludgewith dried bio-solids removed from an exit end of the dryer.

The dried bio-solids can either be stored for future use or incorporateddirectly into the combustion processes of the cement making operation.

Therefore, in a first aspect the present invention is a method fordrying wet bio-solid material for use as a fuel or fuel additive in acement making process by extracting excess heat from a clinker coolingapparatus used in the cement making process; using the excess heatextracted from the clinker cooler to heat a dryer; introducing the wetbio-solid material into the dryer whereby the bio-solids are dried byevaporation of moisture and volatile organic components from the wetbio-solids; condensing water evaporated from the bio-solids for reuse orsafe disposed; recovering volatile organic vapors for introduction intoa combustion process in the cement making process; and recovering adried bio-solid product.

In another aspect the present invention is an apparatus formanufacturing cement, the apparatus having a main rotary kiln, anoptional pre-heater, an optional calciner and a clinker cooler, theimprovement comprising; incorporating into the apparatus means for usingexcess heat generated in the clinker cooler to dry wet bio-solidsmaterial for use as a primary fuel or fuel supplement in the cementmaking apparatus.

In yet another aspect the present invention is an apparatus includingmeans to dry wet bio-solids which includes a contact dryer to dry thebio-solids by direct contact with a heated surface or surfaces, andmeans to heat the surface or surfaces by heat exchange of a heatexchange fluid with excess heat in a cement clinker cooler, the heatexchange fluid being in a closed loop between a heat exchanger in theclinker cooler and internally of the heated surfaces.

In still another aspect the present invention is an apparatus includingmeans to dry wet bio-solids using one of a rotary dryer, rotary tubedryer, vertical flash dryer or a fluidized bed dryer to dry thebio-solids by direct contact with hot gases from a cement clinkercooler.

A major benefit from the present invention resides in the ability toavoid landfill disposal of bio-solid materials that will decay andgenerate methane a known and unwanted atmospheric “Greenhouse Gas”.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic representation of a conventional cement makingprocess.

FIG. 2 a is a schematic drawing of a process and apparatus according toan embodiment of the present invention.

FIG. 2 b is a schematic drawing of a process and apparatus according toanother embodiment of the present invention.

FIG. 3 a is a schematic representation of one method and apparatus forintroducing dried bio-solids into the combustion zone of a cement kiln.

FIG. 3 b is an alternate embodiment of another method and apparatus forintroducing dried bio-solids into the main burner of a cement kiln.

FIG. 3 c is a schematic representation of a method for introducing driedbio-solids directly into a conventional burner of a cement kiln withoutmodification of the main burner.

FIG. 4 a is a schematic representation of a method an apparatus forintroducing dried bio-solids into a calciner using an auxiliary pipe.

FIG. 4 b is a schematic representation of a method and apparatus forintroducing dried bio-solids into a calciner using a conventionalburner.

FIG. 5 is a schematic representation of a method and apparatus forintroduction of dried bio-solids into the loop duct of a preheatingapparatus used in a conventional cement making process and apparatus.

DETAILED DESCRIPTION OF THE INVENTION

Bio-solids, defined as residual by-products from biological activity orthe residual by-product from processing biological material, are ofinterest for use as a fuel or a fuel additive in the manufacture ofcement.

Table 1 sets forth types of materials that would be usable in the methodand apparatus of the present invention.

TABLE 1 Fuel %/Ash % Critical Ash Material Solid %/Liquid % (Dry) FuelBTU's/lb (Dry) Components Sewage Sludge 15/85 70/30 5,000-8,000 P₂O₅, ClPaper Pulp 20/80 70/30 5,000-8,000 Na2O, K2O Industrial Sludges 20/8050/50 5,000-8,000 varies Food Processing 20/80 50/50 5,000-8,000 variesSludges Agri-Waste 20/80 50/50 5,000-8,000 varies Sludges

The foregoing materials are the wettest types of material that can beused in the method and apparatus of the present invention. Materialshaving moisture content above 10% by weight but less than the moisturecontent set out in Table 1 can also be used in the process of thepresent invention.

Of the materials in the foregoing table sewage sludge is the semi-solidresidue of sewage treatment processes.

Paper pulp bio-solids generally consist of organic based by-productsfrom paper manufacturing. Paper manufacturing uses conventional sourcesof cellulose such as wood and flax. Paper manufacturing also usessecondary sources of cellulose such as waste paper and waste cardboard.The manufacturing process requires the grinding, particle sizeclassification, heating, and blending of conventional and secondarysources of cellulose. These processes generate by-products that havevarious concentrations of water and organic components.

Industrial sludges for use in the present invention, contain organicbased by-products with liquid or solid hydro-carbon components.Petroleum tanker sludge, oil soaked clay, oil soaked filter media,sediment from coal washing operations and wet flexi coke are examples ofsuitable industrial sludges.

Food processing sludges are generated from many process operations. Atthe beginning and end of batch processes, off spec materials aregenerated and must be disposed. Similarly, when process equipment isperiodically cleaned or cleaned between batch runs materials aregenerated and must be disposed. These materials generally consist ofgrain and vegetable based products that are being ground, mixed anddosed to produce various food products. In other processes diatomaceousearth filter media often becomes saturated with the organic residuesform mixing, batching, cooking and pasteurizing processes. Thesesaturated filter media materials are suitable bio-solid sludges for theprocesses of the present invention.

Agricultural waste sludges consist of by-products from harvesting andprocessing crops. Materials such as stalks, seeds, shells, pits, skins,rinds, twigs, leaves, and bark with various concentrations of moistureare suitable for the process of the present invention.

According to the present invention the method and apparatus are used toseparate water and organic components from the bio-solid materials.Organic components can be recovered and burned with ash residuechemically incorporated into the cement manufacturing process. Theoverall method and apparatus of the present invention minimizes negativeenvironmental impact from the drying and reuse of the wet bio-solidmaterials.

A conventional cement manufacturing process uses large volumes of rawmaterials such as limestone and coal to produce Portland Cement. Theprocess consists of three main areas, raw meal preparation,pyro-processing, and finished grinding. Limestone (CaCO₂) is generallythe main raw ingredient. Smaller amounts of materials containingalumina, silica and iron are proportioned and ground with limestone toproduce a raw meal. A precisely controlled mixture of raw meal is thenfed to the pyro-processing area. The pyro-processing area burns largeamounts of conventional fuel such as coal, oil and gas to generate thetemperatures required to calcine the limestone and allow the new cementcomponents to form. An intermediate product called clinker is producedin the pyro-processing area. Clinker is cooled from high pyro-processingtemperatures to ambient temperature. A finished grinding process whichincorporates a small percentage of gypsum into the clinker results in aPortland Cement product.

Referring to FIG. 1 a conventional clinkering process is embodied in theapparatus shown as 10. The apparatus 10 includes a preheating section 12which can include a series of preheater stages 14, 16, 18, 20 and 22,which are interconnected with recovery conduits, e.g. 24, wherein theraw meal represented by arrow 25 introduced by a conduit 26 is graduallypreheated for introduction into the main kiln 28 via a conduit 30.Downstream of the preheater section the process apparatus include acalciner 32, which is fired with a conventional burner 34 to begin theconversion of the limestone to clinker. The calciner portion of theprocess can include a loop system 36 which includes a conduit 38 tointroduce additional fuel into the loop system 36 whereby the fines fromthe calciner are recycled and eventually introduced into the main kiln28.

Gases and fine particles exiting the preheater section 12 are sent to acooling tower 32 for cooling of the gases and exhausting via a blower34. Dust is removed in a dust collector 36.

Main kiln 28 includes a main burner 38 which is fired using a fuel suchas coal, oil or natural gas together with an oxygen containing fluidsuch as air. The preheated or pre-calcined meal enters the kiln at afirst or entry end 40. As the meal progresses from the entrance 40 tothe exit 42 of the kiln 28 it is converted into a clinker. The clinkerexits the kiln 28 and is deposited into a clinker cooler 44 where theclinker is cooled to a temperature of about 200° F. Thereafter, theclinker represented by arrow 45 is conducted via a conduit for otherdelivery device 46 to the grinding operation. The clinker cooler 44includes a dust recovery system 48 so that dust can be recycled to thepyro-processing portion of the cement making process.

Referring to FIG. 2 a the apparatus according to one embodiment of thepresent invention is shown incorporated into the conventional cementmaking process in connection with the clinker cooler 44. The method andapparatus of the present invention incorporates a bio-solids unloadingstation 50 wherein the wet bio-solids are unloaded and distributed to acontact dryer 52. The bio-solids unloading station 50 is under a slightnegative pressure so that volatile organic compounds and other odorsfrom the bio-solids being dumped into the unloading station 50 can bewithdrawn by a conduit 54 and introduced into the clinker cooler 44. Theslight negative pressure of the unloading station controls potentialemission from the wet bio-solid material. The bio-solid material isdelivered to the facility in covered dump trailers, e.g. 56 or bladdertrucks. Bladder trucks would be a preferred method because of theability to control odors during transport and unloading of the bio-solidmaterial. A bladder truck contains an internal flexible chamber in whichthe wet bio-solid material would be transported. At the unloading pointa conduit from the bladder would be connected to the receiving hopper ordevice 51 of the unloading station 50. Compressed air or other highpressure fluid would be introduced between the inner flexible chamberand the outer fixed chamber of the bladder truck. Thus the wet bio-solidmaterial will be extruded into the hopper 51 and generation of volatileorganic emissions will be minimized. Any organic vapors from receivinghopper 51 of unloading station 50 will be conducted to the clinkercooler 44 via conduit 58. Additionally, the main introduction point ofunloading station 50 will have a movable cover 60 to facilitateunloading of covered dump trailers. The moveable cover 60 will be keptclosed between unloading events. When covered dump trailers are unloadedmore air will be drawn into the clinker cooler to insure that theseareas continue to have a slight negative pressure and thus odors emittedfrom the wet bio-solid materials are controlled.

A universal unloading station containing both a bladder truck unloadingsystem and a dump trailer unloading system can be constructed to improvethe economics of the overall process.

In the embodiment FIG. 2 a the method and apparatus of the presentinvention includes a closed contact dryer 52. The wet bio-solidmaterials are conducted via a closed feeding system 62, 64 into thedryer 52. The dryer 52 includes contact drying surfaces, which may be inthe form of an auger 66 which is heated by a conduit where heat exchangefluid is introduced into the inner portion of the auger 66. In addition,the outer case 68 of dryer 52 can also be heated, the case beingprovided with a double wall structure (outer jacket) so that heatexchange fluid is introduced between the walls of the double wallportion of the case 68 of dryer 52. A heat exchange fluid is circulatedthrough the auger and the outer jacket and through a heat exchanger 70contained in the exhaust duct system 72, 74 of clinker cooler 44. Theheat exchanger 70 will receive the heat exchange fluid which iscirculated by a blower or pump 76 connected in the closed loop systemincluding heat exchanger 70, dryer 52 and conduits 78 and 80respectively. The heat exchange fluid is heated by the heat of theclinker cooler 44 which may be as high as 1000° F. Normally the clinkerenters the cooler 44 at a temperature greater than 2000° F. and exits ata temperature at about 200° F.

The heat exchange fluid indirectly contacts the wet bio-solid materialswhich are then dried and leave the contact dryer 52 through a valvedconduit 82. The dried bio-solids are transported to a storage facility84 by a pneumatic transport pump 86 and suitable conduit 88. Storagefaculty 84 can be closed bins, silos or the like provided with a dustcollection device 83 and an explosion vent as are known in the art. Thedry bio-solids can be stored and used as necessary in the overallprocess. For example, a first dosing system consisting of a meteringvalve 90, and conduit 92 and pump 94 can be used to withdraw the driedbio-solids from storage bin 84 and conduct them directly to the mainburner 38 of kiln 28 via conduit 92. A second dosing system (meteringvalve 96, pump 98) similar to the first can be used to withdrawbio-solids and conduct them via conduit 100 to the burner 34 containedin the calciner 32.

Referring back to the dryer 52 a collection system 102 removes moistureand volatile organic compound from the dryer 52. The water vapor andvolatile organic compounds are passed into a condenser separator 104,which is cooled by a cooling apparatus 106 as is well known in the art.The condenser/separator 104 permits the water vapor to be condensed toliquid water essentially free of organic components, which is removed byconduit 109 to used in the overall cement making process as needed.

While the foregoing description has reference to a dryer 52 being of thetype using a heated auger and heated casing any type of indirect heatexchange dryer would be suitable. For example, heated tubes inserted ina fluidized bed of wet bio-solids would be suitable for the presentinvention.

Referring to FIG. 2 b the apparatus according to another embodiment ofthe present invention is shown incorporated into the conventional cementmaking process in connection with the clinker cooler 44. The method andapparatus of the present invention incorporates a bio-solids unloadingstation 50 wherein the wet bio-solids are unloaded and distributed to arotary dryer 152. The bio-solids unloading station 50 as is under aslight negative pressure so that volatile organic compounds and otherodors from the bio-solids being dumped into the unloading station 50 canbe withdrawn by a conduit 54 and introduced into the clinker cooler 44.The slight negative pressure of the unloading station controls potentialemission from the wet bio-solid material. The bio-solid material isdelivered to the facility in covered dumped trailers, e.g. 56 or bladdertrucks. Bladder trucks would be a preferred method because of theability to control odors during transport and unloading of the bio-solidmaterial. A bladder truck contains an internal flexible chamber in whichthe wet bio-solid material would be transported. At the unloading pointa conduit from the bladder would be connected to the receiving hopper ordevice 51 of the unloading station 50. Compressed air or other highpressure fluid would be introduced between the inner flexible chamberand the outer fixed chamber of the bladder truck. Thus the wet bio-solidmaterial will be extruded into the hopper 51 and generation of volatileorganic emissions will be minimized. Any organic vapors from receivinghopper 51 will be conducted to the clinker cooler 44 via conduit 58.Additionally, the main introduction point of unloading station 50 willhave a movable cover 60 to facilitate unloading of covered dumptrailers. The moveable cover 60 will be kept closed between unloadingevents. When covered dump trailers are unloaded more air will be drawninto the clinker cooler to insure that these areas continue to have aslight negative pressure and thus odors emitted from the wet bio-solidmaterials are controlled.

A universal unloading station containing both a bladder truck unloadingsystem and a dump trailer unloading system can be constructed to improvethe economics of the overall process.

As illustrated in FIG. 2 b the method and apparatus of the presentinvention will include a direct contact dryer being one of a rotarydryer, rotary tube dryer, vertical flash dryer or a fluidized bed dryer.For the purpose of the description reference will be made to rotarydryer 152. The wet bio-solid materials are conducted via a closedfeeding system 162 to the entry end 156 of rotary dryer 152. Heatedatmosphere which may be as high as 1000° F. from clinker cooler 44 willbe conducted to dryer 152 via a conduit 154 terminating at the entry end156 of dryer 152. Normally the clinker enters the cooler 44 at atemperature greater than 2000° F. and exits at a temperature at about200° F.

The heated atmosphere introduced into dryer 152 directly contacts thewet bio-solid materials which are then dried and leave the dryer 152through a valved conduit 182. The dried bio-solids are transported tothe storage facility 84 by a pneumatic transport pump 86 and suitableconduit 88. Conduit 88 can include a cooling device 89 to remove anyexcess heat from the dried bio-solids. The dry bio-solids can be storedand used as necessary in the overall process. For example, a firstdosing system consisting of a metering valve 90, and conduit 92 and pump94 can be used to withdraw the dried bio-solids from storage bin 84 andconduct them directly to the main burner 38 of kiln 28 via conduit 92. Asecond dosing system (metering valve 96, pump 98) similar to the firstcan be used to withdraw bio-solids and conduct them via conduit 100 tothe burner 34 contained in the calciner 32.

Referring back to the dryer 152, moisture and volatile organic compoundsare removed from the dryer 152 through conduit or device 158. The watervapor and volatile organic compounds are passed into a condenserseparator 104, which is cooled by a cooling apparatus 106 as is wellknown in the art. The condenser/separator 104 permits the water vapor tobe condensed to liquid water essentially free of organic components,which is removed by conduit 107 to be used in the overall cement makingprocess as needed. Cooled atmospheric gases freed of volatile compoundsand water can be removed to the kiln exhaust system 72 via conduit 113.

Volatile organic compounds are recovered from the condenser/separator104 and passed, depending upon volumetric flow, into the inlet of theclinker cooler fans in the clinker cooler 44. Alternatively, thevolatile organic compounds can be recovered in conduit 108 andintroduced into kiln burner 38 by fan or blower 110 where they arecombusted to products of combustion that can be incorporated into theclinker without affecting the properties of the clinker.

A core feature of the drying processes is the use of the closed dryers52 and 152. These devices use heat in the clinker cooler 44 to heat thebio-solid material in a confined space to drive off a controlled amountof moisture either via conduit heat exchange or direct heat exchangewith the bio-solids. In the embodiment of FIG. 2 a a heat exchange fluidis heated by heat exchange in a heat exchanger 70 located in a by-passduct system 72 of the clinker cooler 44 in order to extract the maximumamount of heat from the clinker cooler. Varying the amount of hotclinker cooler gases that are directed through the by-pass system 72will vary the amount of hot thermal fluid generated for introductioninto the dryer 52. Flow rate and temperature of the circulating thermalfluid will determine the maximum amount of water that can be separatedfrom the wet bio-solid material during any given period of time. Themaximum flow rate and temperature of hot thermal fluid will depend uponthe size and efficiency of a given clinker cooler. Depending upon thecomposition of exit gases from the clinker cooler 44 it may be necessaryto use a cyclone separator 112 to remove excessive amounts of fineparticle to prevent excessive build-up on contact surfaces of heatexchanger 70.

In the embodiment of FIG. 2 b the hot gases from the clinker cooler areintroduced into the dryer 152 where they become in direct contact withthe bio-solids in dryer 152.

Water vapor and volatile organic vapors generated by the closed dryers52, 152 will be conveyed to the condenser/separator 104 by maintaining aslight negative pressure in the system. This negative pressure will begenerated by tapping into one of the clinker cooler fan intake ducts orinto the primary air fan intake for the main burner. Thecondenser/separator 104 will remove water vapor from the dryer 52discharge and the negative pressure will convey any volatile organicvapors into the pyro-processing phase of the cement making process.Condensed water vapor can be used for conditioning (cooling) the exhaustgas stream from the pyro-process before it enters the final dustcollector.

The closed dryers will be operated to obtain approximately 10% moisturecontent by weight in the dried bio-solid material when it leaves thedryer. Monitoring the material and vapor discharge temperatures andvarying the temperature of the incoming heat to the dryer makes itpossible to control the moisture content of the dried bio-solids leavingthe dryers. It is possible to reduce the residual moisture content ofthe dried bio-solids below 10%. However, as the moisture content isreduced below 10% it is expected that the dried bio-solids will becomeincreasingly dusty (i.e. finer average particle size). Depending on thetype of bio-solid material being dried, this may or may not be anadvantage in the handling, storage and use of the dried bio-solidmaterial.

As stated above the dried bio-solid material will be pneumaticallyconveyed to a storage device or silo 84. Depending upon the temperature,it may be necessary to either cool the dried bio-solid material in aseparate cooling (heat exchange) device or use a cooled conveying gas totransport the dried bio-solids to the storage silo 84. Any of thesemethods or an alternate method of cooling may be employed to ensure thatthe dried bio-solids are delivered to the storage silo 84 at atemperature of less than 40° C. (less than 104° F.).

It is also within the scope of the invention to introduce driedbio-solid material into the storage device 84 where the material hasbeen dried off site and transported in a pre-dried condition to thecement plant. Bio-solid materials that have been dried off site bythermal, solar or a composting processes can also be used for theirresidual mineral and energy value. Any storage system therefore will bedesigned to accommodate these materials and unload them and use them inthe overall cement making process.

Any storage device must be designed in accordance with all applicablelocal, state and federal codes and regulations to insure safe handlingof such material. It is believed that procedures and methods that areused for the storage and handling of pulverized coal will enable a userto comply with such laws and regulations for storage and handling ofdried bio-solid materials.

Although the storage system will have the ability to withdraw and dosethe dried bio-solid material as needed alternate transport methods maybe practical in some cement processes. Some cement plans have existingpneumatic transport systems for conveying a primary fuel such aspulverized coal. With such a system it is possible to deposit acontrolled flow rate of dried bio-solids directly into an existingpneumatic transport line. In this aspect, the dosing systems woulddischarge through a rotary air lock directly into the pneumatictransport system.

Referring to FIGS. 3 a, 3 b and 3 c the dried bio-solids transported tothe combustion (burning) zone of kiln 28 can be introduced into inseveral ways. If the dried bio-solids are conveyed to the main burningzone of kiln 28 by an independent pneumatic conveying line, a separateburner pipe, e.g. 112 in FIG. 3 a, can be used to introduce the driedbio-solids into the rotary kiln. The nozzle or discharge end 114 of pipe112 can be placed at any location proximate the discharge end or nozzleend 39 of the main burner 38.

As shown in FIG. 3 b the dried bio-solids can be conveyed to the burning(combustion) zone of kiln 28 via an independent pneumatic conveying line116, which terminates in a conduit 118, which is inside of the burner120. Burner 120 can be a multi port or a concentric tube burner, suchburners being well known in the art.

As shown in FIG. 3 c the dried bio-solids can be conveyed directly tothe burner 122 in kiln 28 together with the normal fuel, e.g. pulverizedcoal, as represented by arrow 124 to produce the flame 126 inside thekiln 28.

It should be noted that the particle size of fuels burned in the maincombustion zone of the cement kiln is of critical importance. If toomany large particles of fuel enter this portion of the kiln there is apossibility that some of them may fall into the reaction zone of thekiln and adversely affect the quality of the clinker produced. For thisreason the degree of fineness of the dried bio-solids must be monitoredclosely. As set forth above the particle size of the dried bio-solidswill be a function of the moisture content, which will be adjusted asneeded. If adjusting the moisture content does not yield a sufficientlysmall particle size, it may be necessary to use a mechanical sizereduction (i.e. grinding) device to optimize the size of the driedbio-solids to be used in a combustion zone.

As shown in FIG. 4 a if the dried bio-solids are conveyed to thecalciner 32 via an independent pneumatic conveying line 128 they can beintroduced to the calciner 32 combustion zone with a separate burnerpipe 130 having a discharge end 132, which is proximate the dischargeend 35 of conventional fuel burner 34. Alternatively, as shown in FIG. 4b the dried bio-solids can be conveyed directly to the calciner 32burner 84 via an existing pneumatic conveying line 134 where they wouldmix with the primary fuel (e.g. pulverized coal) and introduced into thecombustion zone through the existing main burner 34.

As shown in FIG. 5 a calciner includes a loop duct (or riser duct) 136.Dried bio-solids can be introduced into duct 136 via a direct pneumatictransport line 138 as shown in FIG. 5.

Contrary to the requirements of the main kiln burner, particle size isnot as critical for dried bio-solids introduced into the calciner andthe loop duct combustion zone of the cement plant. Larger particle sizedried bio-solids can be accommodated in these areas because of thelonger retention time in the combustion zone and the fluidizing effectof high gas flows. Furthermore, any particles or fuel that become mixedwith the raw meal (feed) will have ample time to oxidize before they areadded to the more critical reaction zone of the kiln.

The combustion zone of a cement kiln is one of the hottest industrialprocesses. Gas temperatures in the main combustion zone can exceed 3500°F. Additionally, these gases remain above 1800° F. for as long as 5seconds as they move away from the combustion zone. The combination ofpreheated high oxygen content air, high combustion temperatures and longresidence time above 1800° F. insures complete combustion of all organiccompounds. The calciner loop duct combustion zone consists of the maincalciner combustion chamber and the loop duct or riser duct. Gastemperatures in the calciner combustion chamber can read 2500° F. Thesegases can remain above 1500° F. for as long as five (5) seconds as theyleave the calciner combustion chamber and pass through the loop duct tothe pre-heater cyclone chambers.

The main components of the raw materials used to manufacture cement arecalcium, silica, alumina and iron. The inorganic ash components of driedbio-solids have high concentrations of calcium and silica that cansupplement the conventional minerals. Therefore, the inorganic ashresidue of dried bio-solids can be beneficially recovered byincorporation into the cement clinker. The intimate mixing of thecombustion gases and the cement raw materials as the gases leave thecombustion zone ensure complete integration of inorganic ash residuesinto the conventional raw materials. In this manner the inorganic ashresidues become an integral part of the process chemistry. There areminor constituents in the inorganic ash residue of dried bio-solids thatmust be monitored to insure the quality of the performance of the cementproduct. Trace components in the ash such as P₂O₅, Cl, Na₂O, and K₂Omust be measured on a regular basis to control any potentiallydeleterious effect of these components on the cement manufacturingprocess or the performance of the finished product. Specifically, P₂O₅from dried bio-solids will increase the concentration of potassium inthe finished clinker. Research has indicated that when the level ofpotassium in a clinker approaches 1.5% the setting time of the resultingconcrete will be extended. Additionally, high concentrations of Cl, N₂Oand K₂O from dried bio-solids can cause build up in kiln, which, inturn, can cause operational interruptions.

Having thus described our invention what is desired to be secured byLetters Patent of the United States is set forth in the appended claims.

1. A method for drying wet bio-solid material for use as a fuel or fueladditive in a cement making process comprising the steps of: extractingexcess heat from a clinker cooling apparatus used in said cement makingprocess; exposing said wet bio-solid material to said heat extractedfrom said clinker cooler, whereby said bio-solids are dried byevaporation of moisture and volatile components from said wetbio-solids; condensing water evaporated from said bio-solids for reuseor safe disposed; recovering said volatile vapors for introduction intoa combustion process in said cement making process; and recovering adried bio-solid product.
 2. A method according to claim 1 wherein saidvolatile organic components are introduced into a main burner of a kilnused in said cement making process.
 3. A method according to claim 1wherein said water condensed after evaporation from said bio-solids isused in a gas conditioning step in said cement making process.
 4. Amethod according to claim 1 wherein said dried bio-solid product isinventoried in a storage device.
 5. A method according to claim 4wherein said dried bio-solids are inventoried in a storage device withbio-solids dried off site.
 6. A method according to claim 1 wherein saiddried bio-solids are cooled to 40° C. or 104° F.
 7. A method accordingto claim 1 wherein said recovered bio-solids are used in a maincombustion zone of said cement making process.
 8. A method according toclaim 1 wherein said recovered bio-solids are used in one of a calciner,loop duct combustion zone or both in said cement making process.
 9. Amethod according to claim 1 including using a rotary dryer to heat anddry said wet bio-solids.